Modular fuel cell system

ABSTRACT

A fuel cell stack module includes a base, a cover dome removably positioned on the base, and a plurality of fuel cell stacks removably positioned on the base below the cover dome. A modular fuel cell system includes a plurality of the fuel cell stack modules, where each fuel cell stack module may be electrically disconnected, removed from the fuel cell system, repaired or serviced without stopping an operation of the other fuel cell stack modules in the fuel cell system.

CROSS-REFERENCE TO RELATED PATENT APPLICATIONS

This application is a continuation of U.S. patent application Ser. No.11/656,006, filed Jan. 22, 2007, which claims priority to U.S.Provisional Patent Application No. 60/760,933, filed Jan. 23, 2006, theentire contents of both of which are incorporated herein by reference intheir entirety.

BACKGROUND OF THE INVENTION

The present invention relates generally to the field of fuel cellsystems and more particularly to a modular fuel cell system and methodof operating same.

SUMMARY OF THE INVENTION

Fuel cells are electrochemical devices which can convert energy storedin fuels to electrical energy with high efficiencies. High temperaturefuel cells include solid oxide and molten carbonate fuel cells. Thesefuel cells may operate using hydrogen and/or hydrocarbon fuels. Thereare classes of fuel cells, such as the solid oxide regenerative fuelcells, that also allow reversed operation, such that oxidized fuel canbe reduced back to unoxidized fuel using electrical energy as an input.A large number of prior art fuel cell systems are configured to eitherhave a narrow power generation range or a single operating point. Inorder to achieve installations of different generation capacities,multiples of these systems are installed, which increases the overallcost and complexity.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a three dimensional view of a system of the first embodimentof the invention with a cover dome removed.

FIG. 2 is a schematic side cross sectional view of the system of thefirst embodiment.

FIG. 3 is a top of view of the base of the system of the firstembodiment.

FIGS. 4A and 4B are side cross sectional views of a conduit before andafter a fuse is melted, respectively.

FIG. 5 is a three dimensional view of a system of the second embodimentof the invention

FIGS. 6, 7 and 8 are schematic diagrams of fuel cell systems of theembodiments of the invention.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

The first embodiment of the invention provides a fuel cell stack module1 which is illustrated in FIGS. 1, 2 and 3. The module 1 contains a base3, which comprises a chamber having an interior volume 5 and an uppersurface 7. The base 3 may have a cylindrical shape, with a flat uppersurface and a circular cross section, as shown in FIG. 1. However, thebase 3 may have any other suitable shape, such as a square, rectangular,polygonal, oval or irregular cross section.

Each fuel cell stack module 1 includes at least one fuel cell stack 9and a cover dome 11 covering the stack(s) 9. For example, a single fuelcell stack 9 may be located under the dome 11. Alternatively, two ormore stacks 9 may be located under the dome 11. The stacks 9 may bestacked vertically and/or horizontally under each dome 11. If desired,the vertically stacked fuel cell stacks 9 may be provided in a cascadeconfiguration, where the fuel exhaust stream from one stack is used asthe inlet fuel stream for an adjacent stack.

The stacks 9 may comprise any suitable fuel cells. For example, the fuelcells may comprise solid oxide fuel cells having a ceramic oxideelectrolyte. Other fuel cell types, such as PEM, molten carbonate,phosphoric acid, etc. may also be used. The stacks 9 may compriseexternally and/or internally manifolded stacks. For example, the stacksmay be internally manifolded for fuel and air with fuel and air risersextending through openings in the fuel cell layers and/or in theinterconnect plates between the fuel cells. Alternatively, the fuelcells may be internally manifolded for fuel and externally manifoldedfor air, where only the fuel inlet and exhaust risers extend throughopenings in the fuel cell layers and/or in the interconnect platesbetween the fuel cells. The fuel cells may have a cross flow (where airand fuel flow roughly perpendicular to each other on opposite sides ofthe electrolyte in each fuel cell), counter flow parallel (where air andfuel flow roughly parallel to each other but in opposite directions onopposite sides of the electrolyte in each fuel cell) or co-flow parallel(where air and fuel flow roughly parallel to each other in the samedirection on opposite sides of the electrolyte in each fuel cell)configuration.

The cover dome 11 may have any suitable configuration. For example, thecover dome 11 may have a cylindrical configuration. However, the dome 11may have a polygonal or oval horizontal cross section and/or it may havea tapered rather than flat upper surface. The dome may be made of anysuitable thermally insulating or thermally conductive material, such asmetal, ceramic, etc.

The stack(s) 9 and the dome 11 are removably positioned or removablyconnected to an upper surface 7 of the base 3. Preferably, each fuelcell stack 9 and the cover dome 11 are separately removably connected tothe upper surface 7 of the base 3. In this case, the dome 11 may beeasily removed from the upper surface 7 of the base 3 without removingthe stack(s) 9 under the dome 11. Alternatively, if the dome 11 containsa door or a hatch, then the stack(s) 9 under the dome 11 may be easilyremoved through the door or hatch without removing the dome 11.

The term “removably connected” means that the stack(s) 9 and/or the dome11 are connected to the upper surface 7 of the base 3 in such a way asto be easily removed for repair or servicing. In other words, “removablyconnected” is an opposite of “permanently connected”. For example, thestacks 9 and/or the dome 11 are removably connected to the upper surface7 of the base 3 by at least one of a snap fit connection, a tension fitconnection, a fastening connection or a slide rail connection. Anexample of a snap fit connection is a bayonet type connection in whichone or more prongs which hold a component in place by hooking into anopening are pressed inward or outward to unhook them from the opening.An example of a tension fit connection is where a component, such as astack 9 or a dome 11, is pressed into an opening or groove in thesurface 7 of the base 3 which has the about same size as the crosssection of the stack 9 or the dome 11 such that tension holds the stackor the dome in the opening or groove. An example of a fasteningconnection is connection by a fastener, such as a bolt or a clip, whichcan be removed by service personnel. An example of a slide railconnection is a drawer or dove tail type connection, such as a groove inthe upper surface 7 of the base 3 into which a protrusion in the stack 9can be slid into, or a groove in the bottom stack 9 plate into which aprotrusion in the upper surface 7 of the base 3 can be slid into. Forexample, as shown in FIG. 3, the upper surface 7 of the base 3 maycontain openings 17 for holding the stacks 9 by tension and/or railgrooves 19 for sliding the stacks 9 into place. Other removableconnection types may be used. An example of a permanent connection is awelded connection, such as where the dome 11 is welded to the surface 7of the base.

The stack(s) 9 and the dome 11 be removably connected using a differenttype of connection from each other. Furthermore, in an alternativeaspect of the invention, the dome 11 may be removably connected to theupper surface 7 of the base 3, while the stack(s) 9 may be non-removablyconnected to the same surface 7.

Preferably, at least one heat exchanger is located in the interiorvolume 5 of the base 3. For example, as shown in FIG. 2, for stackswhich are internally manifolded for fuel and air, both fuel 13 and air15 heat exchangers may be located in the interior volume 5 of the base3. For stacks 9 that are internally manifolded for fuel but externallymanifolded for air, the fuel heat exchanger may be located in theinterior volume 5 of the base. The fuel 13 and air 15 heat exchangersprovide heat from the fuel and air exhaust streams, respectively, tofuel and air inlet streams, respectively. The heat exchangers may belocated side by side or stacked vertically in the interior volume 5 ofthe base 3. As shown in FIG. 2, there may be one fuel 13 and one air 15heat exchanger for each module 1. However, if desired, more than onefuel 13 and/or more than one air 15 heat exchanger may be provided.

As shown in FIGS. 2 and 3, the base 3 also contains a plurality of fuelinlet conduits 21 which provide a fuel inlet stream to the fuel cellstacks 9, a plurality of fuel exhaust conduits 23 which remove the fuelexhaust stream from the stacks 9, a plurality of air inlet conduits 25which provide an air (or other oxidizer) inlet stream to the stacks 9,and a plurality of air exhaust conduits 27 which remove the air exhauststream from the stacks 9. A fuel cell stack 9 is removably attached toone of each conduits 21, 23, 25, 27.

As shown in FIG. 2, a fuel inlet line 29 is connected to a first inletof the fuel heat exchanger 13. The plurality of fuel inlet conduits 21are fluidly connected to a first outlet of the fuel heat exchanger 13.The term “fluidly connected” means either directly connected orindirectly connected such that the fuel inlet stream flows from the fuelheat exchanger 13 through one or more other components until it reacheseach fuel inlet conduit 21. The plurality of fuel exhaust conduits 23are fluidly connected to a second inlet of the fuel heat exchanger 13. Afuel exhaust line 31 is connected to a second outlet of the fuel heatexchanger. An air inlet line 33 is connected to a first inlet of the airheat exchanger 15. The plurality of air inlet conduits 25 are fluidlyconnected to a first outlet of the air heat exchanger 15. The pluralityof air exhaust conduits 27 are fluidly connected to a second inlet ofthe air heat exchanger 15. An air exhaust line 35 is connected to asecond outlet of the air heat exchanger 15.

If desired, an optional external fuel reformer 37 may also be providedif the fuel cells of the stacks 9 are of the external reforming type. Ifthe fuel cells of the stacks 9 are of an internal reforming type, thenthe external reformer 37 may be omitted. The reformer may be located onthe upper surface 7 of the base 3 under the dome 11 or inside theinterior volume 5 of the base 3. If the reformer 37 is located on theupper surface 7 of the base 3, then the reformer 37 may also beremovably connected to the upper surface 7 of the base 3. For example,as shown in FIG. 2, a single reformer 37 is used to reform a hydrocarbonfuel, such as natural gas or methane to a hydrogen containing fuel. Afuel conduit 39 may connect the first outlet of the fuel heat exchanger13 with the inlet of the reformer 37. The fuel inlet conduits 21 connectthe outlet of the reformer 37 with the fuel inlets of the stacks 9.

If desired, the reformer 37 may be thermally integrated with the fuelcell stacks 9. The term “thermally integrated” in this context meansthat the heat from the reaction in the fuel cell stacks 9 drives the netendothermic fuel reformation in the reformer 37. The reformer may bethermally integrated with one or more fuel cell stacks 9 by placing thereformer and stack(s) under the same dome 11 and/or in thermal contactwith each other, or by providing a thermal conduit or thermallyconductive material which connects the stack(s) to the reformer. Forexample, the reformer 37 may be located in close proximity to at leastone fuel cell stack 9 to provide radiative and/or convective heattransfer from the stack to the reformer.

Preferably, the base 3 and the dome 11 are also used to provide anelectrical connection from the stacks 9 to the power conditioningequipment. For example, the upper surface of the base may contain aplurality of electrical contacts 41, such as negative or groundelectrical contacts. Each contact 41 is located where a bottom end plateof a fuel cell stack 9 would touch the upper surface 7 of the base 3.Each negative or ground electrode or end plate of each fuel cell stack 9is electrically connected to one of the plurality of electrical contacts41. The base 3 also contains a common electrical bus 43, such as anegative or ground bus 43, which is electrically connected to the fuelcells 9 through the contacts 41.

The dome 11 contains a separate electrical bus 45 for each stack 9. Thebus 45 has a different polarity than the polarity of the commonelectrical bus 43. For example, the dome 11 may have a plurality ofpositive buses 45. A positive electrode or end plate of a fuel cellstack 9 is electrically connected to a respective positive electricalbus 45 extending from the dome 11.

The positive electrode or end plate of each fuel cell stack 9 may beelectrically connected to the respective positive electrical bus 45using any suitable contact or electrical connection. For example, asshown in FIG. 2, an upper interior surface of the dome 11 contains aplurality of electrically conductive pressure members 47. The pressuremembers 47 on the dome 11 are aligned with the stack 9 positions overthe contacts 41 on the upper surface 7 of the base 3. Each pressuremember 47 removably holds at least one fuel cell stack 9 between thecover dome 11 and the upper surface 7 of the base 3. The positiveelectrode or end plate of each fuel cell stack 9 is electricallyconnected to the positive electrical bus 45 through a respectivepressure member 47. The pressure member 47 may be a flexible bar, plateor spring which puts a downward pressure on the stack 9 to keep thestack 9 firmly against the electrical contact 41 on the upper surface 7of the base. When the dome 11 is pushed down to close the module 1, thepressure member flexes to press the stack 9 into place on the base 3.When the dome 11 is removed to service or repair the module, thepressure member releases the stack 9.

Thus, in a system comprising a plurality of modules, each module 1 maybe electrically disconnected, removed from the fuel cell system and/orserviced or repaired without stopping an operation of the other modules1 in the fuel cell system. In other words, each module 1 may beelectrically disconnected, removed from the fuel cell system and/orserviced or repaired while the other modules 1 continue to operate togenerate electricity. Thus, the entire fuel cell system does not have tobe shut down when one stack 9 malfunctions or is taken off line forservicing.

When one module 1 is taken off line (i.e., it is turned off to beremoved, repaired or serviced), while the other modules 1 continue tooperate, the flow of fuel to the module 1 which is taken off line shouldbe stopped. This may be accomplished by placing a high temperature valvein each fuel inlet line 29. The valve may be turned off manually orelectronically to stop the flow of fuel through a given fuel inlet line29, while the fuel continues to flow through the other fuel inlet lines29 to the other modules 1.

In an alternative aspect of the invention, a heat activatable fuse isused instead of the high temperature valve to stop the flow of fuelthrough a given fuel inlet line. Such a fuse may be less expensive thana high temperature valve.

As shown in FIG. 4A, the fuse comprises a low melting point materialcladding 49 located inside the fuel inlet line 29 and an electricheating element 51 which is adapted to heat and melt the cladding 49 toseal the fuel inlet line 29. The fuel inlet line 29 may comprise anysuitable fluid conduit, such as a pipe. For example, the cladding 49 maybe located on one or more interior walls of the conduit such that thefuel inlet stream may flow through the conduit 29 around the cladding49. The cladding may comprise any suitable material which has a highermelting point than the fuel inlet stream temperature, but much lowermelting point than that of the conduit 29, such that the heating element51 can only melt the cladding 49 but not the conduit 29. The heatingelement may comprise any suitable resistance-type or other type (such asoptical-type or RF-type) heating element, such as a nichrome wirewrapped around the outside the portion of the conduit 29 containing thecladding 49. As shown in FIG. 4B, when a current is passed through theheating element 51, the cladding 49 melts to seal the conduit 29 and tostop the flow of the fuel through the conduit 29 without melting theconduit 29. The conduit 29 may be easily replaced once its respectivemodule 1 is repaired or serviced.

Thus, a method of sealing a fluid conduit includes heating a cladding 49of a first material located inside the conduit 29 of a second materialhaving a higher melting point than the first material to melt thecladding 49 such that the melted cladding seals the conduit 29. While afuel inlet line for a fuel cell system is used as an example, the fusemay be used to seal any other liquid or gas carrying conduit, such as apipe or channel, used in any other suitable device.

The second embodiment of the invention provides a modular design for theentire fuel cell system rather than just for the fuel cell stackmodules. The modular system design provides flexible installation andoperation. Modules allow scaling of installed generating capacity,reliable generation of power, flexibility of fuel processing, andflexibility of power output voltages and frequencies with a singledesign set. The modular design results in an “always on” unit with veryhigh availability and reliability. This design also provides an easymeans of scale up and meets specific requirements of customer'sinstallations. The modular design also allows the use of available fuelsand required voltages and frequencies which may vary by customer and/orby geographic region. Thus, in summary, since the fuel cell system isdesigned as a modular set, it can be installed to accommodate therequirements of different customers and the elements of the system areable to work in concert to achieve a very high system reliability andavailability.

FIG. 5 shows an exemplary configuration of the modular fuel cell system60. The system 60 includes the following elements. The system 60includes a plurality of fuel cell stack modules 61. These modules 61 aredevices which contain the components used for generating DC power from areadily reformed fuel stream.

In one aspect of the second embodiment, each fuel cell stack module 61is the same as the module 1 of the first embodiment. Thus, each module61 shown in FIG. 5 may comprise a base 3, a cover dome 11 and one ormore fuel cell stacks 9, as shown in FIG. 2. For example, for a hightemperature fuel cell system, such as a SOFC or a molten carbonate fuelcell system, each fuel cell stack module 61 is the same as the module 1of the first embodiment. In an alternative aspect of the secondembodiment, each module 61 may comprise one base 3 and a plurality offuel cell stacks 9 covered by a plurality of cover domes 11.Alternatively, each module 61 may have a different structure orconfiguration from the modules 1 of the first embodiment. For example,for low temperature fuel cell systems, such as PEM systems, each module61 can be different from the module 1 of the first embodiment. Thus, thesystem of the second embodiment is applicable to high and lowtemperature fuel cell stack modules.

Each module 61 contains at least one fuel cell stack 9. As discussedwith respect to the first embodiment, multiple fuel cell stack modules61 may be installed in a clustered installation, such as for example, ina single hot box 62. A failure of a single fuel cell stack module 61results only in a slightly degraded output capacity or slightly degradedsystem efficiency because the remaining fuel cell stack modules 61continue operation.

The system 60 also contains one or more fuel processing modules 63.These modules are devices which contain the components used forpre-processing of fuel so that it can be readily reformed. The fuelprocessing modules 61 may be designed to process different sets offuels. For example, a diesel fuel processing module, a natural gas fuelprocessing module, and an ethanol fuel processing module may beprovided. The processing modules 63 may processes at least one of thefollowing fuels selected from natural gas from a pipeline, compressednatural gas, propane, liquid petroleum gas, gasoline, diesel, homeheating oil, kerosene, JP-5, JP-8, aviation fuel, hydrogen, ammonia,ethanol, methanol, syn-gas, bio-gas, bio-diesel and other suitablehydrocarbon or hydrogen containing fuels. If desired, the reformer 37may be located in the fuel processing module 63. Alternatively, if it isdesirable to thermally integrate the reformer 37 with the fuel cellstack(s) 9, then the reformer(s) 37 may be located in the fuel cellstack module(s) 61. Furthermore, if internally reforming fuel cells areused, then the external reformer 37 may be omitted entirely.

The system 60 also contains one or more power conditioning modules 65.These modules 65 are devices which contain the components for convertingthe DC power to AC power, connecting to the grid, and managingtransients. The power conditioning modules 65 may be designed convertthe DC power from the fuel cell modules 61 to different AC voltages andfrequencies. Designs for 208V, 60 Hz; 480V, 60 Hz; 415V, 50 Hz and othercommon voltages and frequencies may be provided.

Each type of module 61, 63, 65 may be installed in or on a separatecontainer, such as a box, rack or platform. Thus, the containers may belocated separately from each other, and may be moved, repaired orserviced separately. For example, as shown in FIG. 5, the fuel cellstack modules 61 are located in a common hot box 62. The fuel processingmodule or modules 63 may be located in a separate box 67. The powerconditioning module or modules 65 may be located on a separate rack 69.

Additionally, the modular system 60 may be configured in a way to easeservicing of the system. All of the routinely or high servicedcomponents (such as the consumable components) may be placed in a singlemodule to reduce amount of time required for the service person. Forexample, the purge gas and desulfurizer material for a natural gassystem may be placed in a single module. This would be the only moduleaccessed during routine maintenance. Thus, each module 61, 63, 65 may beserviced, repaired or removed from the system without opening thecontainer in which the other modules are located and without servicing,repairing or removing the other modules. In other words, at least onemodule can be taken off line without taking the remaining modules offline. For example, the system can include a plurality of fuel cell stackmodules 61. When at least one fuel cell stack module 61 is taken offline, the remaining fuel cell stack modules 61, the fuel processingmodule(s) 63 and the power conditioning module(s) 65 are not taken offline. Furthermore, the system may contain a plurality of each type ofmodule 61, 63, 65. When at least one module of a particular type istaken off line, the remaining modules of the same type are not taken offline.

Furthermore, if desired, the system may be configured such that one ofseveral optional modules is selected for each of fuel processing, fuelcell, and power conditioning. Thus, before or after the system isinstalled to generate power, the fuel processing modules may beinterchanged without modification to the fuel cell modules or to thepower conditioning modules, while the power conditioning modules may beinterchanged without modification to the fuel cell modules or to thefuel processing modules.

If desired, the system may include a single user interface, such as acomputer or other suitable control terminal or panel. The user interfaceallows the operator to control or operate all of the modules of thesystem from a single location. However, if desired, each type of modulemay have a separate user interface as a back-up or for separate controlof the module.

In one aspect of the second embodiment, the system 60 contains four fuelcell stack modules 61 in the hot box 62. Each fuel cell stack module 61may be designed to have ¼ the capacity of the total modules 61 in thesystem 60. Each module 61 may be designed to have two-side access andalso to be “indexed” allowing four fuel cell stack modules 61 to beplaced in 90-degree rotations in a single installation. For example, thehot box 62 may have doors 64 on two or more adjacent sides. When bothadjacent doors of the hot box are open, a module 61 located in thatcorner of the hot box can be accessed from two sides for service orrepair. To access one of the other three modules though the open doors,the base or stage below the modules 61 is rotated 90 degrees.

For example, when each module 61 is a 25 kW module, a set of fourmodules provides a densely populated 100 kW system. Larger systems coulduse this same configuration where individual fuel cell modules have a100 kW capacity and a clustered installation of four such modules wouldhave 400 kW capacity.

While four modules 61 and a four sided hot box 62 are illustrated inFIG. 5, it should be understood that the system 60 may contain less thanfour or more than four modules 61. Furthermore, the hot box 62 may havefive or more sides or it may have a cylindrical or oval shape.Furthermore, the hot box 62 may have more than two doors and may have adoor on each side.

The system 60 provides a high system reliability and availability.Because the clustered system continues to generate power when there is afailure of a single generation module, the reliability of the system asa whole is quite high. The system 60 also provides a flexibility forinstallation. The fuel cell system can be tailored to fit the specificrequirements of a large variety of installations because many optionsfor fuel processing and power conditioning are provided.

The system also allows a low cost, high volume fuel cell moduleproduction. Because the fuel cell stack module 61 is designed as acommon element of the clustered system, it does not need to besubstantially modified in order to accommodate different fuels ordifferent output voltages or frequencies. These modifications areaccommodated in the fuel processing 63 or power conditioning 65 modules.Because of the single fuel cell module design, engineering costs areminimized. Examples of these costs include characterization testing,reliability testing, environmental testing, and certification typetesting.

The system also provides a module upgrading capability. By dividing thesystem functionality into discrete modules, the system may be upgradedas new versions of the product are made available. These upgrades may bemade by replacing individual modules instead of the entire product. Thusthe cost of such upgrades is minimized. Furthermore, capacity upgradescan be made by adding fuel cell modules. Fuel flexibility upgrades canbe made by adding or changing fuel processing module.

The system also provides a flexibility in module sizes. The fuel cellmodule subsystem and the power conditioning subsystem can be based onmodules of different sizes. For instance, fuel cell module subsystem canbe based on 25 kW modules while the power conditioning subsystem can bebased on 100 kW modules. The architecture can have enough redundancy toavoid single point failures.

The system also provides an ease of design and testing for productcertification to accepted design standards. By placing fuel cell andfuel processing components in separate modules, the gas handlingrequirements of these modules need not be applied to the powerconditioning module. Likewise, the high voltage requirements of thepower conditioning module need not be applied to the fuel cell and fuelprocessing modules.

The modular fuel cell systems of the first and the second embodimentsmay contain the components described and illustrated below with respectto the third, fourth, fifth or sixth embodiments. However, it should benoted that the fuel cell systems may contain different components andconfigurations than those described and illustrated with respect to thethird, fourth, fifth or sixth embodiments below. The third, fourth,fifth and sixth embodiments describe and illustrate a schematic ofvarious fuel cell systems, such as a solid oxide fuel cell system, wherethe fuel exhaust stream is separated into two streams and one of thestreams is recycled into the fuel inlet stream. It should be noted thatfuel cell systems other than solid oxide fuel cell systems may also beused.

In the system of the third embodiment, a portion of the fuel cell stackfuel exhaust stream is directly recycled into the fuel inlet stream.Another portion of the fuel cell stack fuel exhaust stream is providedinto a partial pressure adsorption apparatus, and the separated hydrogenis then recycled into the fuel inlet stream and/or is provided to ahydrogen storage vessel or to a hydrogen using device.

FIG. 6 illustrates a fuel cell system 100 of the third embodiment. Thesystem 100 contains a fuel cell stack 101, such as a solid oxide fuelcell stack (illustrated schematically to show one solid oxide fuel cellof the stack containing a ceramic electrolyte, such as yttria stabilizedzirconia (YSZ) or scandia stabilized zirconia (SSZ), an anode electrode,such as a nickel-YSZ or Ni-SSZ cermet, and a cathode electrode, such aslanthanum strontium manganite (LSM)). It should be noted that the stack101 may correspond to one of the stacks 9 located in the fuel cell stackmodule 1 of the first embodiment.

The system also contains a partial pressure swing adsorption (“PPSA”)unit 401 comprising a plurality of adsorbent beds (not shown forclarity). The PPSA unit 401 acts as a regenerative dryer and carbondioxide scrubber. The PPSA unit 401 is described in U.S. patentapplication Ser. Nos. 10/188,118 and 10/188,120, both filed on Jul. 25,2005 and both incorporated herein by reference in their entirety.

The system 100 also contains the first conduit 403 which operativelyconnects a fuel exhaust outlet 103 of the fuel cell stack 101 to a firstinlet 402 of the partial pressure swing adsorption unit 401. Forexample, the first inlet 402 may comprise a feed valve and/or an inletto one of the adsorbent beds. The system 100 also contains the secondconduit 405 which operatively connects a purge gas source, such as adried or atmospheric air source 406 to a second inlet 404 of the partialpressure swing adsorption unit 401. The purge gas source 406 maycomprise an air blower or compressor and optionally a plurality oftemperature swing cycle adsorption beds.

The system also contains a third conduit 407 which operatively connectsan outlet 408 of the partial pressure swing adsorption unit 401 to thehydrogen storage vessel or to the hydrogen using device. If desired, thethird conduit 407 also operatively connects an outlet 408 of the partialpressure swing adsorption unit 401 to a fuel inlet 105 of the fuel cellstack 101, as will be described in more detail below. Preferably, thesystem 100 lacks a compressor which in operation compresses the fuelcell stack fuel exhaust stream to be provided into the partial pressureswing adsorption unit 401.

The system 100 also contains the fourth conduit 409 which removes theexhaust from the unit 401. The conduit 409 may be connected to acatalytic burner 107 or to an atmospheric vent. Optionally, the burner107 may also be operatively connected to the stack fuel exhaust outlet103 to provide a portion of the fuel exhaust stream into the burner 107to sustain the reaction in the burner.

The system 100 also contains an optional selector valve 108, such as amulti-way valve, for example a three-way valve. The selector valve 108has an inlet operatively connected to an outlet of the partial pressureswing adsorption unit 401, a first outlet operatively connected to thehydrogen storage vessel or to the hydrogen using device, and a secondoutlet operatively connected to a fuel inlet 105 of the fuel cell stack101. In operation, the valve 108 divides the hydrogen containing streamprovided from the PPSA unit 401 into a first stream, which is providedinto the hydrocarbon fuel inlet stream, and a second stream which isprovided to the hydrogen storage vessel or to the hydrogen using device.However, the valve 108 may be omitted and the system 100 may beconfigured to provide the entire hydrogen containing stream into thehydrocarbon fuel inlet stream, or to the hydrogen storage vessel or tothe hydrogen using device, if such optional vessel or device areconnected to the system 100.

Preferably, the second outlet of the selector valve 108 is operativelyconnected to the fuel inlet line 29 of the fuel cell stack 101 via ablower or a heat driven compressor 109. The device 109 has an inletwhich is operatively connected to the partial pressure swing adsorptionunit 401 (via the selector valve 108) and an outlet which is operativelyconnected to a fuel inlet 105 of the fuel cell stack 101. For example,conduit 407 connects the blower or compressor 109 to the unit 401 viathe selector valve 108. In operation, the blower or compressor 109controllably provides a desired amount of hydrogen and carbon monoxideseparated from a fuel cell stack fuel exhaust stream into the fuel cellstack fuel inlet stream. Preferably, the device 109 provides thehydrogen and carbon monoxide into a fuel inlet line 29 which isoperatively connected to the a fuel inlet 105 of the fuel cell stack101. Alternatively, the device 109 provides the hydrogen and carbonmonoxide directly into the fuel inlet 105 of the fuel cell stack 101.

The system 100 also contains a condenser 113 and water separator 115having an inlet which is operatively connected to a fuel cell stack fuelexhaust 103 and an outlet which is operatively connected to an inlet 402of the partial pressure swing adsorption unit 401. The condenser 113 andwater separator 115 may comprise a single device which condenses andseparates water from the fuel exhaust stream or they may compriseseparate devices. For example, the condenser 113 may comprise a heatexchanger where the fuel exhaust stream is cooled by a cool counter orco-flow air stream to condense the water. The air stream may comprisethe air inlet stream into the fuel cell stack 101 or it may comprise aseparate cooling air stream. The separator 115 may comprise a water tankwhich collects the separated water. It may have a water drain 117 usedto remove and/or reuse the collected water.

The system 100 also contains a recuperative heat exchanger 121 whichexchanges heat between the stack fuel exhaust stream and the hydrocarbonfuel inlet stream being provided from the inlet line 29. The heatexchanger 121 may be the same as the fuel heat exchanger 13 of the firstembodiment. The heat exchanger helps to raise the temperature of thefuel inlet stream and reduces the temperature of the fuel exhaust streamso that it may be further cooled in the condenser and such that it doesnot damage the humidifier.

If the fuel cells are external fuel reformation type cells, then thesystem 100 contains a fuel reformer 37. The reformer 37 reforms ahydrocarbon fuel inlet stream into hydrogen and carbon monoxidecontaining fuel stream which is then provided into the stack 101. Thereformer 37 may be heated radiatively, convectively and/or conductivelyby the heat generated in the fuel cell stack 101 and/or by the heatgenerated in an optional burner/combustor, as described in U.S. patentapplication Ser. No. 11/002,681, filed Dec. 2, 2004, incorporated hereinby reference in its entirety. Alternatively, the external reformer 37may be omitted if the stack 101 contains cells of the internal reformingtype where reformation occurs primarily within the fuel cells of thestack.

Optionally, the system 100 also contains an air preheater heat exchanger125. This heat exchanger 125 heats the air inlet stream being providedto the fuel cell stack 101 using the heat of the fuel cell stack fuelexhaust. If desired, this heat exchanger 125 may be omitted.

The system 100 also preferably contains an air heat exchanger 127. Theheat exchanger 127 may be the same as the air heat exchanger 15 of thefirst embodiment. This heat exchanger 127 further heats the air inletstream being provided to the fuel cell stack 101 using the heat of thefuel cell stack air (i.e., oxidizer or cathode) exhaust. If thepreheater heat exchanger 125 is omitted, then the air inlet stream isprovided directly into the heat exchanger 127 by a blower or other airintake device.

The system may also contain an optional water-gas shift reactor 128. Thewater-gas shift reactor 128 may be any suitable device which converts atleast a portion of the water and carbon monoxide in the fuel exhauststream into free hydrogen and carbon dioxide. For example, the reactor128 may comprise a tube or conduit containing a catalyst which convertssome or all of the carbon monoxide and water vapor in the fuel exhauststream into carbon dioxide and hydrogen. Thus, the reactor 128 increasesthe amount of hydrogen in the fuel exhaust stream. The catalyst may beany suitable catalyst, such as a iron oxide or a chromium promoted ironoxide catalyst. The reactor 128 may be located between the fuel heatexchanger 121 and the air preheater heat exchanger 125.

Optionally, the system 100 is operatively connected to a hydrogenstorage vessel 129 or a hydrogen using device 131. However, the vessel129 or device 131 may be omitted and the system 100 may be used to onlyproduce electricity rather than electricity and hydrogen together. Thehydrogen storage vessel may comprise a hydrogen storage tank or ahydrogen dispenser. The vessel may contain a conduit leading to ahydrogen using device which is used in transportation, power generation,cooling, hydrogenation reactions, or semiconductor manufacture. Forexample, the system 100 may be located in a chemical or a semiconductorplant to provide primary or secondary (i.e., backup) power for the plantas well as hydrogen for use in hydrogenation (i.e., passivation ofsemiconductor device) or other chemical reactions which require hydrogenthat are carried out in the plant.

The hydrogen using device 131 may also comprise another fuel cell system(such as a fuel cell stack), such as low temperature fuel cell system,such as a proton exchange membrane (PEM) fuel cell system, which useshydrogen as a fuel. Thus, the hydrogen from the system 100 is providedas fuel to one or more additional fuel cells 131. For example, thesystem 100 may be located in a stationary location, such as a buildingor an area outside or below a building and is used to provide power tothe building. The additional fuel cells 131 may be located in vehicleslocated in a garage or a parking area adjacent to the stationarylocation. A vehicle may comprise a car, sport utility vehicle, truck,motorcycle, boat or any other suitable fuel cell powered vehicle. Inthis case, the hydrocarbon fuel is provided to the system 100 togenerate electricity for the building and to generate hydrogen which isprovided as fuel to the fuel cell system 131 powered vehicles. Thegenerated hydrogen may be stored temporarily in the hydrogen storagevessel 129 and then provided from the storage vessel to the vehicle fuelcells 131 on demand (analogous to a gas station) or the generatedhydrogen may be provided directly from the system 100 to the vehiclefuel cells 131 through a conduit.

The system 100 may contain an optional hydrogen conditioner. Thehydrogen conditioner may be any suitable device which can purify, dry,compress (i.e., a compressor), or otherwise change the state point ofthe hydrogen-rich gas stream provided from the PPSA unit 401. Ifdesired, the hydrogen conditioner may be omitted.

The hydrogen using device 131 may comprise a PEM fuel cell system oranother similar device which is generally carbon monoxide intolerant.Thus, carbon monoxide has to be scrubbed (i.e., removed by gasseparation and/or chemical reaction) from the hydrogen rich stream beingprovided from the PPSA unit 401 before the hydrogen rich stream isprovided into the PEM fuel cells located in a vehicle or into another COintolerant device 131.

In this case, the system 100 contains an optional carbon monoxidescrubbing device 133. The device 133 contains an inlet operativelyconnected to an outlet of the partial pressure swing adsorption unit 401and an outlet operatively connected to a PEM fuel cell system 131located in a vehicle. In operation, the carbon monoxide scrubbing device133 scrubs carbon monoxide being provided with the hydrogen from thepartial pressure swing adsorption unit 401 and provides the hydrogeneither directly or indirectly to the PEM fuel cell system 131.

The carbon monoxide scrubbing device 133 may comprise any device whichremoves carbon monoxide from the hydrogen rich stream by adsorption,chemical reaction and/or any other suitable method. The device 133 maycomprise a pressure swing adsorption unit and/or a Sabatier reactor. Forexample, as shown in FIG. 6, the scrubbing device comprises a Sabatierreactor 135 and a carbon monoxide polisher 137. The Sabatier reactorcomprises a tube or another container which contains a catalyst, such asa platinum family metal on an alumina support. Preferably, the catalystcomprises ruthenium. A gas mixture consisting primarily of hydrogen andcarbon monoxide is introduced into reactor tube from the PPSA system 401and contacts the catalyst therein. The gas mixture undergoes animmediate exothermic reaction and converts the carbon monoxide and someof the hydrogen to methane and water vapor. Remaining carbon monoxide isthen additionally scrubbed from the hydrogen, methane and water vaporgas stream in the polisher 137, which may comprise a silver basedadsorption device which adsorbs carbon monoxide. The polisher maycomprise plural adsorption beds where one bed adsorbs carbon monoxidewhile other beds are being regenerated. The outlet stream containinghydrogen, methane and water vapor from the polisher is then provided tothe hydrogen storage vessel 129 or the hydrogen using device 131 (theseparate purge gas outlet from the polisher 137 is not shown forclarity). The hydrogen may be used as the fuel in the PEM fuel cellsystem 131, the water vapor may be used to humidify the PEM electrolyteand the methane simply acts as a diluting gas in a PEM system.

Alternatively, the carbon monoxide scrubbing device 133 may comprise apressure swing adsorption (“PSA”) unit. This unit is similar to the PPSAunit 401, except that a reciprocating compressor is used to pressurizethe feed gas into one or more adsorbent beds which contain a materialwhich selectively adsorbs carbon monoxide compared to hydrogen. Thepressure swing adsorption unit may operate on a Skarstrom-like PSAcycle. The classic Skarstrom cycle consists of four basic steps:pressurization, feed, blowdown, and purge. For example, the PSA unit maycontain two adsorbent beds. When one bed is undergoing pressurizationand feed by the compressor, the other column is undergoing blowdown andpurge. Three-way valves may be used to direct the feed, purge andproduct gases between the beds.

Alternatively, the optional device 131 may comprise a carbon monoxidetolerant electrochemical cell, such as a stack of high-temperature,low-hydration ion exchange membrane cells. This type of cell includes anon-fluorinated ion exchange ionomer membrane, such as, for example, apolybenzimidazole (PBI) membrane, located between anode and cathodeelectrodes. The membrane is doped with an acid, such as sulfuric orphosphoric acid. An example of such cell is disclosed in US publishedapplication US 2003/0196893 A1, incorporated herein by reference in itsentirety. A stack 131 of these cells may be operated in a fuel cell modeto generate electricity for a vehicle or other uses when hydrogen isprovided to the cells of the stack. These cells are carbon monoxidetolerant and operate in a temperature range of above 100 to about 200degrees Celsius. Thus, the hydrogen containing stream is preferablyprovided to the stack 131 at a temperature above about 120 degreesCelsius. If a carbon monoxide tolerant device 131 is used, then thecarbon monoxide scrubbing device 133 is preferably omitted.

The system 100 also contains a fuel splitter device 201, such as acomputer or operator controlled multi-way valve, for example a three-wayvalve, or another fluid splitting device. The device 201 contains aninlet 203 operatively connected to the fuel cell stack fuel exhaustoutlet 103, a first outlet 205 operatively connected to the condenser113 and water separator 115 and a second outlet 207 operativelyconnected to the fuel cell stack fuel inlet 105. For example, the secondoutlet 207 may be operatively connected to the fuel inlet line 29, whichis operatively connected to inlet 105. However, the second outlet 207may provide a portion of the fuel exhaust stream into the fuel inletstream further downstream.

Preferably, the system 100 contains a second blower or compressor 209which provides the fuel exhaust stream into the fuel inlet stream.Specifically, the outlet 207 of the valve 201 is operatively connectedto an inlet of the blower or compressor 209, while an outlet of theblower or compressor 209 is connected to the hydrocarbon fuel inlet line29. In operation, the blower or compressor 209 controllably provides adesired amount of the fuel cell stack fuel exhaust stream into the fuelcell stack fuel inlet stream. In one aspect of this embodiment, thedevice 209 is a low temperature blower which operates at a temperatureof 200 degrees Celsius or less. In this case, the heat exchangers 121and 125 lower the temperature of the fuel exhaust stream to 200 degreesCelsius or less to allow the use of the low temperature blower 209.

The system 100 of the third embodiment operates as follows. A fuel inletstream is provided into the fuel cell stack 101 through fuel inlet line29. The fuel may comprise any suitable fuel, such as a hydrocarbon fuel,including but not limited to methane, natural gas which contains methanewith hydrogen and other gases, propane or other biogas, or a mixture ofa carbon fuel, such as carbon monoxide, oxygenated carbon containinggas, such as methanol, or other carbon containing gas with a hydrogencontaining gas, such as water vapor, H₂ gas or their mixtures. Forexample, the mixture may comprise syngas derived from coal or naturalgas reformation.

The fuel inlet stream is combined with a portion of the fuel exhauststream such that hydrogen and humidity (i.e., water vapor) from the fuelexhaust stream is added to the fuel inlet stream. The humidified fuelinlet stream then passes through the fuel heat exchanger 121 where thehumidified fuel inlet stream is heated by the fuel cell stack fuelexhaust stream. The heated and humidified fuel inlet stream is thenprovided into a reformer 37, which is preferably an external reformer.For example, reformer 37 may comprise a reformer described in U.S.patent application Ser. No. 11/002,681, filed on Dec. 2, 2004,incorporated herein by reference in its entirety. The fuel reformer 37may be any suitable device which is capable of partially or whollyreforming a hydrocarbon fuel to form a carbon containing and freehydrogen containing fuel. For example, the fuel reformer 37 may be anysuitable device which can reform a hydrocarbon gas into a gas mixture offree hydrogen and a carbon containing gas. For example, the fuelreformer 37 may comprise a catalyst coated passage where a humidifiedbiogas, such as natural gas, is reformed via a steam-methane reformationreaction to form free hydrogen, carbon monoxide, carbon dioxide, watervapor and optionally a residual amount of unreformed biogas. The freehydrogen and carbon monoxide are then provided into the fuel (i.e.,anode) inlet 105 of the fuel cell stack 101. Thus, with respect to thefuel inlet stream, which is located upstream of the reformer 37 which islocated upstream of the stack 101.

The air or other oxygen containing gas (i.e., oxidizer) inlet stream ispreferably provided into the stack 101 through a heat exchanger 127,where it is heated by the air (i.e., cathode) exhaust stream from thefuel cell stack. If desired, the air inlet stream may also pass throughthe condenser 113 and/or the air preheat heat exchanger 125 to furtherincrease the temperature of the air before providing the air into thestack 101.

Once the fuel and air are provided into the fuel cell stack 101, thestack 101 is operated to generate electricity and a hydrogen containingfuel exhaust stream. The fuel exhaust stream (i.e., the stack anodeexhaust stream) is provided from the stack fuel exhaust outlet 103 intothe partial pressure swing adsorption unit 401. At least a portion ofhydrogen contained in the fuel exhaust stream is separated in the unit401 using a partial pressure swing adsorption. The hydrogen separatedfrom the fuel exhaust stream in the unit 401 is then provided into thefuel inlet stream and/or to the hydrogen storage vessel 129 or thehydrogen using device 131.

The fuel exhaust stream is provided into the unit 401 as follows. Thefuel exhaust stream may contain hydrogen, water vapor, carbon monoxide,carbon dioxide, some unreacted hydrocarbon gas, such as methane andother reaction by-products and impurities. For example, the fuel exhaustmay have a flow rate of between 160 and 225 slpm, such as about 186 toabout 196 slpm, and may comprise between about 45 to about 55%, such asabout 48-50% hydrogen, about 40 to about 50%, such as about 45-47%carbon dioxide, about 2% to about 4%, such as about 3% water and about1% to about 2% carbon monoxide.

This exhaust stream is first provided into the heat exchanger 121, whereits temperature is lowered, preferably to less than 200 degrees Celsius,while the temperature of the fuel inlet stream is raised. If the airpreheater heat exchanger 125 is present, then the fuel exhaust stream isprovided through this heat exchanger 125 to further lower itstemperature while raising the temperature of the air inlet stream. Thetemperature may be lowered to 90 to 110 degrees Celsius for example.

The fuel exhaust stream is then separated into at least two streams bythe device 201. The first fuel exhaust stream is provided toward device209 which recycles this first stream into the fuel inlet stream, whilethe second fuel exhaust stream is directed toward the PPSA unit 401where at least a portion of hydrogen contained in the second fuelexhaust stream is separated using the partial pressure swing adsorption.At least a portion of the hydrogen separated from the second fuelexhaust stream is then provided to the hydrogen storage vessel 129 orthe hydrogen using device 131, and/or a portion of the hydrogen andcarbon monoxide separated from the second fuel exhaust stream areprovided into the fuel inlet stream in the fuel inlet line 29. Forexample, between 50 and 70%, such as about 60% of the fuel exhauststream may be provided to the second blower or compressor 209, while theremainder may be provided toward the PPSA unit 401.

Preferably, the fuel exhaust stream is first provided through the heatexchanger 121, reactor 128 and heat exchanger 125 before being providedinto the valve 201. The fuel exhaust stream is cooled to 200 degreesCelsius or less, such as to 90 to 180 degrees, in the heat exchanger 125prior to being provided into the valve 201 where it is separated intotwo streams. This allows the use of a low temperature blower 209 tocontrollably recycle a desired amount of the first fuel exhaust streaminto the fuel inlet stream, since such blower may be adapted to move agas stream which has a temperature of 200 degrees Celsius or less.

The first fuel exhaust stream is provided into the second blower orcompressor 209 which recycles this stream into the fuel inlet stream.The device 209 may be computer or operator controlled and may vary theamount of the fuel exhaust stream being provided into the fuel inletstream depending on any suitable parameters, which include: i) detectedor observed conditions of the system 100 (i.e., changes in the systemoperating conditions requiring a change in the amount of hydrogen or COin the fuel inlet stream); ii) previous calculations provided into thecomputer or conditions known to the operator which require a temporaladjustment of the hydrogen or CO in the fuel inlet stream; iii) desiredfuture changes, presently occurring changes or recent past changes inthe operating parameters of the stack 101, such as changes in theelectricity demand by the users of electricity generated by the stack,changes in price for electricity or hydrocarbon fuel compared to theprice of hydrogen, etc., and/or iv) changes in the demand for hydrogenby the hydrogen user, such as the hydrogen using device, changes inprice of hydrogen or hydrocarbon fuel compared to the price ofelectricity.

Furthermore, the second blower or compressor may be operated in tandemwith the first blower or compressor 109. Thus, the operator or computermay separately vary the amount of hydrogen being provided into vessel129 or device 131, the amount of hydrogen and carbon monoxide beingprovided into the fuel inlet stream by the first blower or compressor109, and the amount of fuel exhaust stream being provided into the fuelinlet stream by the second blower or compressor 209 based on anysuitable criteria, such as the ones described above. Furthermore, thecomputer or operator may take into account both the amount of hydrogenand carbon monoxide being provided into the fuel inlet stream by thefirst blower or compressor 109 and the amount of fuel exhaust streambeing provided into the fuel inlet stream by the second blower orcompressor 209 and optimize the amount of both based on the criteriadescribed above.

The second fuel exhaust stream is provided from the valve 201 into thecondenser 113 where it is further cooled to condense additional watervapor from the fuel exhaust stream. The fuel exhaust stream may becooled in the condenser by the fuel cell stack air inlet stream or by adifferent air inlet stream or by another cooling fluid stream. The watercondensed from the fuel exhaust stream is collected in the liquid statein the water separator 115. Water may be discharged from the separator115 via conduit 117 and then drained away or reused.

The remaining fuel exhaust stream gas is then provided from theseparator 115 as the feed gas inlet stream into inlet 402 of the partialpressure swing adsorption unit 401 via conduit 403. Furthermore, thepurge gas inlet stream, such as a dried air stream is provided into theunit 401 from blower or compressor 406 through conduit 405 into inlet404. If desired, the air stream may be dried using additional adsorbentbeds in a temperature swing adsorption cycle before being provided intoadsorbent beds of the unit 401. In this case, the heated air used in thetemperature swing adsorption cycle to dry the silica gel or alumina inthe adsorbent beds may be removed from unit 401 via a vent conduit 139.

Thus, the second fuel exhaust stream comprises hydrogen, carbonmonoxide, water vapor, carbon dioxide as well as possible impurities andunreacted hydrocarbon fuel. During the separation step in unit 401, atleast a majority of the water vapor and carbon dioxide in the fuelexhaust stream are adsorbed in at least one adsorbent bed while allowingat least a majority of the hydrogen and carbon monoxide in the fuelexhaust stream to be passed through the at least one adsorbent bed.Specifically, unpressurized fuel exhaust stream is provided into thefirst adsorbent bed to adsorb at least a majority of the water vapor andcarbon dioxide remaining in the fuel exhaust stream in the firstadsorbent bed until the first adsorbent bed is saturated, while thesecond adsorbent bed is regenerated by providing air having a relativehumidity of 50% or less at about 30 degrees Celsius through the secondadsorbent bed to desorb adsorbed carbon dioxide and water vapor. Afterthe first bed is saturated with carbon dioxide, the unpressurized fuelexhaust stream is provided into the second adsorbent bed to adsorb atleast a majority of the remaining water vapor and carbon dioxide in thefuel exhaust stream in the second adsorbent bed until the secondadsorbent bed is saturated while regenerating the first adsorbent bed byproviding air having a relative humidity of 50% or less at about 30degrees Celsius through the first adsorbent bed to desorb the adsorbedcarbon dioxide and water vapor.

The hydrogen and carbon monoxide separated from the fuel exhaust stream(i.e., feed gas outlet stream) are then removed from unit 401 throughoutlet 408 and conduit 407 and provided into the optional selector valve108. The valve 108 divides the hydrogen containing stream provided fromthe PPSA unit 401 into a first stream, which is provided into thehydrocarbon fuel inlet stream in the inletline 29, and a second streamwhich is provided to the hydrogen storage vessel 129 or the hydrogenusing device 131.

The valve 108 may divide the hydrogen containing stream intocontemporaneous first and second streams, such that the first and thesecond streams are provided from the valve 108 at the same time. Thevalve 108 may vary the ratio of how much of the hydrogen containingstream provided from the PPSA unit 401 is provided into a first streamand how much of the hydrogen containing stream is provided into thesecond stream over time. Alternatively, the valve 108 may alternatebetween providing at least 90-100% of the hydrogen containing streaminto the hydrocarbon fuel inlet stream and providing 90 to 100% of thehydrogen containing stream to the hydrogen storage vessel 129, forexample. If desired one of the steams may be omitted and the valve 108may simply constantly direct the hydrogen containing stream into eitherthe vessel 129/device 131 or into the fuel inlet line 29.

The valve 108 may be operated by a computer and/or by an operator tocontrollably provide a desired amount of hydrogen into the fuel inletstream and/or to one of the hydrogen storage vessel and the hydrogenusing device. The computer or operator may vary this amount based on anysuitable parameter. The parameters include: i) detected or observedconditions of the system 100 (i.e., changes in the system operatingconditions requiring a change in the amount of hydrogen or CO in thefuel inlet stream); ii) previous calculations provided into the computeror conditions known to the operator which require a temporal adjustmentof the hydrogen or CO in the fuel inlet stream; iii) desired futurechanges, presently occurring changes or recent past changes in theoperating parameters of the stack 101, such as changes in theelectricity demand by the users of electricity generated by the stack,changes in price for electricity or hydrocarbon fuel compared to theprice of hydrogen, etc., and/or iv) changes in the demand for hydrogenby the hydrogen user, such as the hydrogen using device, changes inprice of hydrogen or hydrocarbon fuel compared to the price ofelectricity, etc.

The second hydrogen rich stream may be provided directly to vessel 129or device 131 or it may first be provided through the carbon monoxidescrubbing device 133 to scrub carbon monoxide from the second streambefore providing the stream to a carbon monoxide intolerant device. Forexample, the second hydrogen stream may be first provided to thehydrogen storage vessel 129 and then provided from the hydrogen storagevessel 129 to the hydrogen using device, such as a PEM fuel cell system131 in a vehicle, on demand or according to a predefined schedule.Alternatively, the second hydrogen stream may be provided to thehydrogen using device, such as a PEM fuel cell system 131 without firstbeing provided to the hydrogen storage vessel 129.

The first hydrogen rich stream provided from the selector valve isrecycled into the fuel inlet stream in the fuel inlet line 29.Preferably, this first hydrogen rich stream containing hydrogen andcarbon monoxide is first provided into a blower or compressor 109, whichis then used to controllably provide a desired amount of hydrogen andcarbon monoxide separated from the fuel exhaust stream into the fuelinlet stream. The blower or compressor 109 may be operated by a computeror by an operator to controllably provide a desired amount of hydrogenand carbon monoxide into the fuel inlet stream, and may vary this amountbased on any suitable parameter. The parameters include: i) detected orobserved conditions of the system 100 (i.e., changes in the systemoperating conditions requiring a change in the amount of hydrogen or COin the fuel inlet stream); ii) previous calculations provided into thecomputer or conditions known to the operator which require a temporaladjustment of the hydrogen or CO in the fuel inlet stream; and/or iii)desired future changes, presently occurring changes or recent pastchanges in the operating parameters of the stack 101, such as changes inthe electricity demand by the users of electricity generated by thestack, etc. Thus, the blower or compressor may controllably vary theamount of hydrogen and carbon monoxide provided into the fuel inletstream based on the above described and/or other criteria. Since thehydrogen and carbon monoxide are cooled to 200 degrees Celsius or less,a low temperature blower may be used to controllably provide thehydrogen and carbon monoxide into the line 29. If desired, the selectorvalve 108 and the blower or compressor 109 may be omitted and the entirehydrogen rich stream may be provided from the PPSA unit 401 to thehydrogen storage vessel 129 or the hydrogen using device 131.

The purge gas outlet stream from the PPSA unit may contain a traceamount of hydrogen and/or hydrocarbon gases trapped in the void volumesof the adsorbent beds. In other words, some trapped hydrogen orhydrocarbon gas may not be removed into conduit 407 by the flush steps.Thus, it is preferred that conduit 409 provide the purge gas outletstream from PPSA unit 401 to a burner 107. The stack 101 air exhauststream is also provided through heat exchanger 127 into the burner 107.Any remaining hydrogen or hydrocarbon gas in the purge gas outlet streamis then burned in the burner to avoid polluting the environment. Theheat from the burner 107 may be used to heat the reformer 37 or it maybe provided to other parts of the system 100 or to a heat consumingdevices outside the system 100, such as a building heating system.

Thus, with respect to the fuel exhaust stream, the heat exchanger 121 islocated upstream of the heat exchanger 125, which is located upstream ofthe condenser 113 and water separator 115, which is located upstream ofthe PPSA unit 401, which is located upstream of blower or compressor 109which is located upstream of the fuel inlet line 29.

If desired, the system 100 may be used together with a humidifier. Sucha system could then be operated in different modes to optimizeelectricity generation or to optimize hydrogen production for thehydrogen storage vessel 129 or the hydrogen using device 131. The systemmay be switched between different modes depending on the demand forand/or price of electricity and hydrogen or other factors.

The humidifier may having a first inlet operatively connected to ahydrocarbon fuel source, such as the hydrocarbon fuel inlet line 29, asecond inlet operatively connected to the valve 201, a first outletoperatively connected to the fuel cell stack fuel inlet 105, and asecond outlet operatively connected to the condenser 113 and waterseparator 115. In operation, the fuel humidifier humidifies ahydrocarbon fuel inlet stream from line 29 containing the recycledhydrogen and carbon monoxide using water vapor contained in a fuel cellstack fuel exhaust stream. The fuel humidifier may comprise a polymericmembrane humidifier, such as a Nafion® membrane humidifier, an enthalpywheel or a plurality of water adsorbent beds, as described for examplein U.S. Pat. No. 6,106,964 and in U.S. application Ser. No. 10/368,425,both incorporated herein by reference in their entirety. For example,one suitable type of humidifier comprises a water vapor and enthalpytransfer Nafion® based, water permeable membrane available from PermaPure LLC. The humidifier passively transfers water vapor and enthalpyfrom the fuel exhaust stream into the fuel inlet stream to provide a 2to 2.5 steam to carbon ratio in the fuel inlet stream. The fuel inletstream temperature may be raised to about 80 to about 90 degrees Celsiusin the humidifier.

When the system is operated to optimize electricity generation (i.e., tooptimize the AC electrical efficiency of the system), the selector valve108 provides the entire hydrogen rich stream from the PPSA unit 401 backinto the fuel inlet conduit. The valve 201 provides a portion of thefuel exhaust stream into the fuel inlet line 29 to humidify the fuelinlet stream. In this case, the valve 201 may route the fuel exhauststream into the fuel inlet conduit to by-pass the humidifier. The perpass fuel utilization rate is maximized to the highest reasonableoperating value, such as about 75% to about 80%, for example, tooptimize the electricity production. In this case, no hydrogen isprovided to the hydrogen storage vessel 129 or to the hydrogen usingdevice 131.

When the system is operated to optimize hydrogen generation for thehydrogen storage vessel 129 or to the hydrogen using device 131, theselector valve 108 provides the entire hydrogen rich stream from thePPSA unit 401 to the hydrogen storage vessel 129 or to the hydrogenusing device 131. No hydrogen rich stream is provided into the fuelinlet conduit. In this case, the valve 201 provides the entire fuelexhaust stream from the stack into the humidifier where the fuel inletstream is humidified, rather than providing a portion of the fuelexhaust stream into the fuel inlet line 29. The per pass fuelutilization rate is minimized to the lowest reasonable operating value,such as about 55% to about 60%, for example, to optimize the hydrogenproduction. In this case, a maximum amount of hydrogen is provided tothe hydrogen storage vessel 129 or to the hydrogen using device 131.Furthermore, more hydrocarbon fuel may be provided to the fuel cellstack when the system operates to optimize hydrogen production than whenthe system operates to optimize electrical efficiency. For example,50-100% more hydrocarbon fuel is provided to the stack 101 when thesystem is operating to optimize hydrogen production than when the systemis operating to optimize electrical efficiency.

The system may also be operated to balance electrical efficiency andhydrogen production. In this case, the selector valve 108 splits thehydrogen rich stream from the PPSA unit 401 between the fuel inlet line29 and the hydrogen storage vessel 129/hydrogen using device 131. Bothsteams may be provided at the same time or the valve may alternatebetween providing the first and the second streams. The amount ofhydrogen provided between the two streams can be varied depending on theconditions described above. In this case, the valve 201 may provide thefuel exhaust stream into the fuel inlet stream and/or into thehumidifier 119, depending on the desired parameters.

FIG. 7 illustrates a system 300 according to the fourth embodiment ofthe invention. The system 300 is similar to system 100, except that thePPSA unit 401, the condenser 113 and water separator 115 are replacedwith an electrochemical hydrogen pump 301. The pump 301electrochemically separates hydrogen from the fuel exhaust stream.

The electrochemical pump 301 may comprise any suitable proton exchangemembrane device comprising a polymer electrolyte. The hydrogen diffusesthrough the polymer electrolyte under an application of a potentialdifference between anode and cathode electrodes located on either sideof the electrolyte. Preferably, the electrochemical pump comprises astack of carbon monoxide tolerant electrochemical cells, such as a stackof high-temperature, low-hydration ion exchange membrane cells. Thistype of cell includes a non-fluorinated ion exchange ionomer membrane,such as, for example, a polybenzimidazole (PBI) membrane, locatedbetween anode and cathode electrodes. The membrane is doped with anacid, such as sulfuric or phosphoric acid. An example of such cell isdisclosed in US published application US 2003/0196893 A1, incorporatedherein by reference in its entirety. These cells operate in atemperature range of above 100 to about 200 degrees Celsius. Thus, theheat exchangers 121 and 125 preferably keep the fuel exhaust stream at atemperature of about 120 to about 200 degrees Celsius such as about 160to about 190 degrees Celsius. FIG. 7 does not illustrate for clarity thevalve 108 and hydrogen storage vessel 129 or the hydrogen using device131. However, these devices may be used in the system 300 if desired.Since the pump 301 provides a hydrogen stream that lacks a substantialamount of carbon monoxide, the CO scrubber 135 is not required to beused with the pump 301 and the hydrogen is provided into the fuel inletstream without the carbon monoxide.

The method of operating the system 300 is similar to the method ofoperating the system 100, except that the fuel exhaust stream isprovided directly from valve 201 into the electrochemical pump 301,which electrochemically separates the hydrogen from the fuel exhauststream. Furthermore, the blower or compressor 109 may be omitted if thepump 301 is capable of controllably providing a desired amount ofhydrogen into the fuel inlet stream. In the method of the fourthembodiment, the effective fuel utilization rate is about 94% and theelectrical efficiency is about 58% when the per pass fuel utilizationrate is 75%, 60% of the fuel exhaust stream is recycled into the fuelinlet stream by valve 201 and about 85% of the hydrogen is recoveredfrom the remaining fuel exhaust stream by pump 301 and recycled into thefuel inlet stream.

In a fifth embodiment of the invention, a temperature swing adsorption(“TSA”) unit is used to separate hydrogen from the fuel exhaust streaminstead of the PPSA unit 401. A TSA unit also does not require the feedgas to be pressurized.

The TSA unit also contains a plurality of adsorbent beds of materialwhich preferentially adsorbs carbon dioxide and water vapor to hydrogenand carbon monoxide. The fuel exhaust stream is provided to at least onefirst adsorbent bed which is maintained at room temperature or other lowtemperature to adsorb at large portion of carbon dioxide and water vaporfrom the fuel exhaust stream. When the first beds is saturated withcarbon dioxide and water vapor, the fuel exhaust stream is switched toat least one second adsorbent bed. The first bed is then purged torelease the adsorbed carbon dioxide and water vapor by increasing thetemperature of the first bed. For example, the first bed may be heatedby heat provided by the fuel cell stack, such as by providing the hotstack cathode air exhaust in heat exchange with the first bed. Afterpurging, the first bed is then cooled with ambient air heat exchange.The cycle continues through the multiple beds to provide a constantrecovery and circulation of the fuel. This embodiment is also amenableto the sequestration of carbon dioxide.

Rather than providing air in heat exchange with (i.e., adjacent to) thebeds, the hot cathode exhaust may be directed through the adsorbent bedsdirectly (with no separate heat exchanger) to discharge the carbondioxide and water vapor. Then cool ambient air is passed directlythrough the beds to condition the beds for the next cycle. If desired, asmall quantity of nitrogen may be is purged through the beds before andafter the bed is reconditioned for additional carbon dioxide and wateradsorption. The nitrogen is obtained from a small temperature swingadsorption device using air as the working fluid.

If desired, the TSA effluent, such as the carbon dioxide and water vaporcontaining effluent, may be discharged to ambient or removed via avacuum pump after the purge gas is stopped. The vacuum removes more ofthe residual carbon dioxide and water (a process akin to pressure-swingadsorption, and commonly referred to as vacuum-swing adsorption) whichmight offer a less expensive and faster means to cool the bed than mightbe achieved using cool air or heat exchange. The use of the vacuum mayalso be amenable to the sequestration of carbon dioxide.

FIG. 8 illustrates a system 400 according to the sixth embodiment of theinvention. The system 400 is similar to system 100, except that the PPSAunit 401 and the blower or compressor 109 are omitted. FIG. 8 alsoillustrates the location of the hot box 62 which may contain one or morefuel cell stack modules 1 or 61 of the first or second embodiments.Furthermore, FIG. 8 shows the location of the optional base 3 of thefirst embodiment.

If desired, a steam generator 303 may also be added to the system 400.The steam generator 303 is provided with water from a water source, suchas a water tank and/or from the condenser 113 and water separator 115,and converts the water to steam. The steam is mixed with the inlet fuelstream in a mixer 305. The steam generator may be heated by a separateheater and/or by the hot cathode exhaust stream and/or by the lowquality heat generated by the burner 107. Furthermore, the low qualityheat generated by the burner 107 may be used to heat the reformerinstead of or in addition to heating the steam generator 303. Theexhaust products of the burner 107 may be provided into the air inletstream directed into the fuel cell stack. The steam generator 303 andthe air preheater 125 may be located in a separate hot box annex whichis placed in contact with the hot box 62. For example, the hot box annexmay comprise a separate container located on top of the hot box. Itshould be noted that the above described features may also be providedinto the systems 100 and 300 of FIGS. 6 and 7.

The method of operating the system 400 is similar to the method ofoperating the system 100, except that the second fuel exhaust streamprovided from valve 201 is not subjected to hydrogen separation.Instead, the second fuel exhaust stream provided from the valve 201 iseither vented or provided to the burner 207. This system 400 is thussimpler than the systems of the prior embodiments, since it does notinclude hydrogen separation steps and equipment.

The method of operating the system 400 allows the use of a lowtemperature blower 209 by cooling the fuel exhaust stream to about 90 to110 degrees Celsius in heat exchangers 121 and 125. In the method of thesixth embodiment, the electrical efficiency is about 54% when the perpass fuel utilization rate is 75% and 60% of the fuel exhaust stream isrecycled into the fuel inlet stream by valve 201.

The fuel cell systems described herein may have other embodiments andconfigurations, as desired. Other components may be added if desired, asdescribed, for example, in U.S. application Ser. No. 10/300,021, filedon Nov. 20, 2002, in U.S. Provisional Application Ser. No. 60/461,190,filed on Apr. 9, 2003, and in U.S. application Ser. No. 10/446,704,filed on May 29, 2003 all incorporated herein by reference in theirentirety. Furthermore, it should be understood that any system elementor method step described in any embodiment and/or illustrated in anyfigure herein may also be used in systems and/or methods of othersuitable embodiments described above, even if such use is not expresslydescribed.

The foregoing description of the invention has been presented forpurposes of illustration and description. It is not intended to beexhaustive or to limit the invention to the precise form disclosed, andmodifications and variations are possible in light of the aboveteachings or may be acquired from practice of the invention. Thedescription was chosen in order to explain the principles of theinvention and its practical application. It is intended that the scopeof the invention be defined by the claims appended hereto, and theirequivalents.

What is claimed is:
 1. A modular fuel cell system, comprising: at leastone fuel cell stack module; at least one fuel processing module; and atleast one power conditioning module, wherein: the modular fuel cellsystem is configured such that at least one module can be taken off linewithout taking the remaining modules off line; each type of module isinstalled in or on a separate container; and the containers are locatedseparately from each other.
 2. The system of claim 1, wherein eachmodule is configured to be serviced, repaired or removed from the systemwithout opening the containers in which the other type of modules arelocated and without servicing, repairing or removing the other type ofmodules.
 3. The system of claim 2, wherein each module is configured tobe accessed from two or more sides.
 4. The system of claim 3, wherein aplurality of the fuel cell stack modules are configured to be indexed tobe accessed from two or more sides.
 5. The system of claim 3, wherein aplurality of the fuel cell stack modules are located in a hot box havingdoors on two or more adjacent sides.
 6. The system of claim 1, wherein:the system is configured such that one of several optional modules isselected for each of fuel processing, fuel cell, and power conditioning;the fuel processing modules may be interchanged without modification tothe fuel cell modules or to the power conditioning modules; and thepower conditioning modules may be interchanged without modification tothe fuel cell modules or to the fuel processing modules.
 7. The systemof claim 2, wherein all high service or consumable components arelocated in a single module.
 8. The system of claim 1, further comprisinga single user interface which is adapted to operate the at least onefuel cell stack module, the at least one fuel processing module, and theat least one power conditioning module.
 9. The system of claim 7,wherein a purge gas and desulfurizer material is located in a singlemodule.